Method and apparatus for discharging polymerization reactors

ABSTRACT

A method and an apparatus of discharging polymer from a continuously operated gas phase reactor, wherein at least one monomer is polymerized in a bed containing active catalyst formed by catalyst and polymer particles suspended in a fluid, the bed defining a fluidized bed level in said reactor. The invention comprises continuously withdrawing polymer powder from the reactor; and adjusting the discharge rate of the polymer powder so as to maintain a constant bed level during polymerization. By means of the invention the discharge of the polymer can be made truly continuous without any disturbance of the polymerization. The rate of withdrawn polymer can be flexibly adjusted depending on the progress of the polymerization and it can also easily be scaled up if the capacity of the reactor is increased.

This application is the national phase under 35 U.S.C. §371 of PCTInternational Application No. PCT/FI99/00941 which has an Internationalfiling date of Nov. 12, 1999, which designated the United States ofAmerica and was published in English.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to a method of producing polymers in acontinuously operated polymerization reactor. In particular, theinvention concerns a method of continuously withdrawing solid polymerpowder from a fluidized bed polymerization reactor with high throughput.The present invention also concerns an apparatus for continuouswithdrawal of polymer powder from a fluidized bed polymerizationreactor.

2. Description of Related Art

A number of processes for preparing polymers in a fluidized bed reactorare known in the art. Such processes are described in e.g. EP PatentSpecification No. 0 517 868, U.S. Pat. No. 4,543,399 and EP PatentApplication No. 0 381 364. The processes are primarily designed for theproduction of polyethylene but they can also be modified for preparingother polyolefins, such as polypropylene. In the process described in EPPatent Specification No. 0 517 868 the fluidized bed reactor acts as asecond reactor in a two-reactor train, in the other above-mentionedprocesses it is a stand-alone reactor.

Conventional gas phase fluidized bed reactors comprise an elongatedreactor body generally having a vertical central axis. The monomers arepolymerized in a fluidized bed above a fluidization grid located in thebottom end of the reactor body. A gaseous stream containing monomer, andoptionally alpha-olefin comonomer(s), hydrogen and inert gas(es) isintroduced to the bottom of the bed through the fluidization grid. Theunreacted gas is collected from the top of the bed, cooled and recycledto the bottom of the reactor. The polymer product is withdrawn from thelower part of the reactor above the fluidization grid. Active catalystis introduced into the bed, either as a fresh catalyst or as polymerparticles from a prior polymerization stage, wherein the active catalystis dispersed.

The polymerization system of a gas phase reactor used for polymerizationof α-olefins comprises a fluidized bed consisting of polymer particlescontaining the active catalyst within, and a gaseous reaction medium.The bed can be maintained in the fluidized state by mechanically mixingor stirring the contents of the reactor and additionally oralternatively by blowing the monomer(s), i.e. the olefin(s), and/or aninert reaction medium (e.g. nitrogen and/or an easily volatilehydrocarbon) into it in a gaseous state. In the case of a fluidized bedprocess, the velocity of the gas needs to be sufficient to support orfluidize the polymer particles. The monomer(s) and/or an inert reactionmedium in liquid state can be introduced into the polymerization systemand the polymerization can be carried out while gasifying saidmonomer(s) and/or reaction medium. The unreacted monomer(s) and/or inertreaction medium can be partly or wholly liquefied and recycled in liquidstate into the polymerization system, as disclosed in EP-A1 0 024 933.

As disclosed in a U.S. Pat. No. 4,803,251, sheet formation isoccasionally encountered in gas phase reactors. The sheets are particleagglomerates having a thickness of about 6 to 15 mm, length of about 30to 150 cm and width of 7.5 to 45 cm or more. The sheets consist of fusedpolymer. According to U.S. Pat. No. 4,803,251, the formation of sheetsis associated with static electricity. The possible formation of hotspots, which eventually may lead to chunk formation as disclosed in EP 0089 691, was also discussed.

Conventionally, the withdrawal of the polymer product from a gas phasereactor is carried out batch-wise. A typical batch discharge processconsists of the following steps: When the surface level within the gasphase reactor rises as a result of polymerization, polymer powder isdischarged through an on/off valve to an outlet tank. A part of thefluidizing gas entering the tank with powder is recycled by a compressorback to the fluidized bed. The degassed powder is recovered andoptionally subjected to further processing.

By means of the batch-wise discharge system described above it ispossible to remove not only the polymer powder but also lumps formed inthe reactor, because the outlet nozzles of the system have a largediameter, generally much larger than required by the withdrawal of thepowder.

There are, however, some serious disadvantages associated withconventional technology. The batchwise discharge is a rather complicatedsystem. It comprises several phases and a number of on/off valves, whichtypically operate tens of times an hour. There has to be at least twodischarge systems, in large plants even more. This feature makes thebatch-wise discharge system rather expensive as an investment and alsothe maintenance is cost-consuming. The complexity of the system alsomakes it vulnerable; if the discharge system becomes clogged or there isa serious failure in the system, the whole plant has to be shut down.

Further, the batch-wise discharge is inflexible because it is difficultto increase its capacity when the capacity of the whole plant isincreased. Instead, a major rise in the production capacity requires theaddition of a new expensive discharge system.

As regards the operation of the system, it can be noted that there is adistinct fluctuation in the bed level when a batch of the polymerproduct is withdrawn from the reactor. This fluctuation influences themonomer concentration and, thus, also other parameters, such as theconcentration of hydrogen and comonomers, which all taken together havea strong impact on the quality of the polymer product.

The discontinuous operation of the outlet system also leads to apulsating operation of the recycle gas compressor. This, again, leads toincreased wear.

Some alternative systems for withdrawal of polymer powder from afluidized bed reactor are also described in the art. Such processes aredescribed in EP Published Patent Applications Nos. 0 006 288 and 0 245043 and U.S. Pat. No. 4,495,337.

The last-mentioned document discloses a process for bottom drainage of afluid-bed reactor, in which the reactor is provided not only with avertical bottom pipe but also with a lateral evacuation pipe locatedabove the distribution plate of the reactor. The side pipe makes itpossible to evacuate a part of the polymer formed in the reactor.According to the reference, to empty the reactor, first all the fractionof polymer powder located above the level of the outlet pipe isdischarged by means of the lateral pipe, then total drainage of thereactor is carried out via the vertical bottom pipe.

EP A1 0 006 288 and A1 0 245 043 disclose discharge systems which arediscontinuously or continuously operated. In EP A1 0 006 288 thedischarge is effected via a dipleg, which passes from the top of thereactor to a point near the bottom. The dip leg is connected to anon/off valve, which is opened intermittently. When the valve is open, amixture of polymer and monomer is passed on to a cyclone in which mostof the monomer vapour is separated from the polymer. The monomer can berecycled to the reactor via compressor.

EP A1 0 245 043 teaches an apparatus for degassing and pelletingpolyolefins, in which there is an outlet nozzle which is equipped with alock chamber placed between two valves activated alternately. Themixture of gas and solid particles, withdrawn from the reactor, istreated in a primary degasser for separating the solid phase from a partof the gas phase accompanying the particles. The gases containingmonomers are recycled into the reactor by a pipe.

Although the prior art suggests that the above three alternativedischarge systems can be not only periodically operated but alsocontinuously, none of them is in fact adapted for such operation. Itshould be noted that the control valves described in EP A1 0 006 288 andA1 0.245 043 are actually intermittently operated which means that thereis no continuous stream of polymer powder through the outlet nozzles.Thus, these systems are merely improved batch discharge systems, whichhave the same main disadvantages as described above. The dischargesystem of U.S. Pat. No. 4,495,337 is, on the other hand, suitable fordraining of the whole content of the reactor rather than for allowingfor continuous withdrawal of polymer powder.

JP-A-58/113208 discloses a process for continuously polymerizing olefinsin vapour phase. The level of the fluidized bed is determined bymeasuring the pressure difference between two specified locations in thebed. The document further indicates that the polymer can be withdrawneither continuously or intermittently. How the suggested continuouswithdrawal is made in practice is not disclosed.

EP-A-0 870 539 discloses an apparatus for polymerizing olefins in gasphase. FIG. 2 and column 8, lines 21-55 of the document describe anembodiment, wherein the polymer is withdrawn continuously from thereactor. The document does not refer to the presence of any chunks orsheets among the polymer, and does not suggest how these should behandled when withdrawing polymer from the reactor. It merely discusseshow the gas discharge pipe should be installed to prevent it fromblocking.

SUMMARY OF THE INVENTION

It is an object of the present invention to eliminate the problemsrelated to the prior art of polymer powder discharge systems and toprovide a simple discharge method with high throughput, which is capableof stabilizing fluidized bed polymerization reactor control anddownstream equipment operation.

Another object of the present invention is to provide a discharge systemwith low investment cost and substantially reduced maintenance cost.

These and other objectives, together with the advantages thereof overknown processes, which shall become apparent from the followingspecification, are accomplished by the invention as hereinafterdescribed and claimed.

The present invention is based on the concept of polymerizing at leastone monomer in a gas phase reactor by continuously feeding a monomerinto a bed formed by catalyst polymer particles suspended in a fluid anddefining a bed level-in the reactor. According to the inventionfree-flowing polymer powder is continuously with-drawn through adischarge pipe, while simultaneously monitoring the surface level of thefluidized bed within a gas phase reactor, and controlling the flow ofmaterial through the pipe depending on the surface level so as tomaintain an essentially constant bed level. To achieve this aim, the gasphase reactor is provided with an outlet nozzle which is equipped with acontinuously operated control valve for the powder discharge. Thecontrol signal for the control valve comes from a fluidized bed levelcontroller. The bed level is typically measured with a pressuredifference or radio-active device.

Further, the present invention comprises withdrawing and separately(continuously or discontinuously) recovering particle agglomerates fromthe reactor.

The discharge system comprises an outlet nozzle, a control valve and abed level indicator. Preferably the system further comprises acollecting vessel placed in communication with the outlet pipe forseparating gas from solid material. The particle agglomerates are eitherwithdrawn directly from the reaction via a separate outlet or theagglomerates are separated from the continuous flow of polymer powder.

More specifically, the method according to the present invention ischaracterized by what is stated in the characterizing part of claim 1.

The apparatus according to the present invention is an apparatus fordischarging polymer from a continuously operated gas phase reactor,wherein at least one monomer is polymerized in a bed containing activecatalyst formed by catalyst and polymer particles suspended in a fluid,said bed defining a fluidized bed level in said reactor, said apparatuscomprising

-   -   an outlet nozzle communicating with the fluidized bed of the gas        phase reactor,    -   a collecting vessel placed in communication with the outlet        nozzle for separating gas from solid material, with a screen for        collecting the lumps and a separate discharge nozzle for the        lumps;    -   a continuously operating valve for adjusting the amount of        polymer powder withdrawn from the reactor via the outlet nozzle;        and    -   means for controlling the operation of the valve for adjusting        the discharge rate of the polymer powder so as to maintain a        constant bed level during polymerization.

The present invention provides considerable advantages. Thus, thedischarge of the polymer can be made truly continuous without anydisturbance of the polymerization. The rate of withdrawn polymer can beflexibly adjusted depending on the progress of the polymerization and itcan also easily be scaled up if the capacity of the reactor isincreased. Further, it has been observed that a mixture of gas andpolymer can pass through the continuously operating control valve. Sucha mixture can be used for pneumatically conveying polymer powder. Also,it has been observed that less reaction gas is discharged than withbatchwise systems.

Particularly well the continuous outlet system is suited to a processwhere the outlet from the gas phase reactor is either directly orindirectly fed into another gas phase reactor. This avoids the controlupsets in the next gas phase reactor due to the sequential powder feed.

Generally, it has not been deemed possible to achieve continuousdischarge because in particular in a PE reactor there are formedconsiderable amounts of lumps and clogs and the size of a continuouslyoperating outlet nozzle is so small that such lumps will eventuallycause clogging thereof. By the present invention it is possible to avoidsaid problem.

Next, the invention will be examined more closely with reference to theattached drawings and a detailed description.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows in a schematically fashion a first embodiment of theinvention comprising a fluidized bed reactor with an outlet nozzle, apipe, a continuously operated control valve provided with means forflushing of the valve, and a processing section for separating gascontaining unreacted monomers from the polymer powder; and

FIG. 2 depicts in a schematically fashion a second embodiment of thepresent invention comprising a fluidized bed reactor with an outletnozzle, a collecting vessel, a control valve operated under the controlof a level indicator, and a processing section for separating gascontaining unreacted monomers from the polymer powder.

DETAILED DESCRIPTION OF THE INVENTION

According to the invention, the present method is used for dischargingpolymer from a continuously operated gas phase reactor, wherein at leastone monomer is polymerized in a bed containing catalyst and polymerparticles suspended in a fluid, said bed defining a fluidized bed levelin said reactor. The catalyst can be fed into the gas phase reactor as astream comprising polymer and active catalyst together with reactionmedium. Such a stream can be obtained from a slurry reactor, such as aloop reactor.

The method comprises continuously withdrawing polymer powder from thereactor and adjusting the discharge rate of the polymer powder so as tomaintain a constant bed level during polymerization. As mentioned above,the discharge rate of the polymer powder is adjusted by using acontinuously operated control valve. Preferred examples of suchcontinuously operated valves are ball valves, V-ball valves and hosevalves.

To ensure stable operation of the process, the polymer powder should befree-flowing. The flow properties of the polymer produced in the processdepend on the average particle size, particle size distribution andespecially shape of the polymer particles. These properties furtherdepend on the corresponding properties of the catalyst used in theprocess. To achieve good flow properties, the polymer particles shouldhave an average particle size between 150 and 4,000 microns, preferablybetween 200 and 2,000 microns. The particle size distribution should besuch that no more than 30%, preferably no more than 15% by weight of theparticles should have a diameter smaller than 100 microns. Moreover, thepolymer particles should have a smooth surface and a regular appearance.Preferably the particles should have a spherical or near sphericalshape.

Together with or separately from the free-flowing polymer powder,polymer agglomerates are also withdrawn from the reactor and recovered.They may be discarded or milled and mixed with the ready polymer.Polymer “particle agglomerates” are particles having a minimum thickness(in any dimension) of at least about 6 mm, in particular about 6 to 15mm. They consist of polymer particles which are at least partially fusedtogether. The agglomerates comprise sheets, chunks and lumps formedduring polymerization, in particular in the gas phase reactor. Asmentioned above, polymer agglomerates will be formed in particularduring polymerization of ethylene.

The apparatus comprises an outlet nozzle communicating with thefluidized bed of the gas phase reactor, a collecting vessel placed incommunication with the outlet nozzle for separating gas from solidmaterial; a continuously operating valve for adjusting the amount ofpolymer powder withdrawn from the reactor via the outlet nozzle; andmeans for controlling the operation of the valve for adjusting thedischarge rate of the polymer powder so as to maintain a constant bedlevel during polymerization. The continuously operating valve ispreferably connected to the collecting vessel. Polymer agglomerates maybe withdrawn from the reactor using a discharge line with adiscontinuously operated discharge valve. Alternatively, polymeragglomerates are separated from the polymer powder in a collectingvessel provided with a screen for isolating the lumps, sheets or clogs.

A first preferred embodiment of the invention is shown in FIG. 1. In thedrawing, the following reference numerals are used:

-   1. gas phase reactor-   2. outlet nozzle of gas phase reactor-   3. control valve-   4. level indicator/controller-   5. discharge line-   7. collecting vessel-   8. flush gas-   12. valve regulating the flow of polymer powder-   18 product receiver or second reactor-   20 gas surge drum-   21 compressor

As shown in the drawing, polymer formed in the reactor 1 is withdrawnfrom a point below the bed level, via an outlet nozzle 2 and a controlvalve 3 together with a sufficient amount of gas for conducting thepolymer to a degassing vessel 18 or to a subsequent reactor. Theoperation of the control valve 3 is controlled by the levelindicator/controlling means 4. The gas separated from the polymer powderin the degassing section is recycled after the separation of the polymerto the gas phase reactor, as indicated by the arrow, and/or to arecovery section.

The continuous withdrawal is preferably used as a single dischargesystem in case of a reactor wherein the amount of lumps is small. Theformation of lumps can be reduced by adding various antistatic agents orby avoiding feeding fresh catalyst to the gas phase reactor, as in amultistep process. A particularly preferred multi-step process isrepresented by the system disclosed in EP Patent Specification No. 0 517868, which comprises in combination a loop reactor and a gas phasereactor.

Even in this embodiment, it is advantageous to place the outlet nozzle 2at a point where no or practically no lumps are present. To that aim thepolymer powder can be continuously withdrawn from a point above afluidization plate, since the lumps tend to accumulate on thefluidization plate. When a gas phase reactor is used, wherein thefluidized bed comprises a mechanically mixed bed, the polymer powder ispreferably withdrawn from said mixed zone.

In order to reduce the risk of clogging of the discharge system, theoutlet nozzle can be provided with a grid (not shown) flush mounted atthe reactor wall to prevent lumps from entering the pipe. The term“flush mounted” means that the grid is installed so that it is at thesame level as the surface of the inner wall of the reactor. It must notextend from the wall surface to the reactor, otherwise it would becovered with polymer. Also, it must not leave a pocket at the nozzlewhich would allow accumulation of polymer there. Further the dischargeline 5 and the control valve 3 can be discontinuously back flushed witha flushing gas flow through gas conduit 8 to prevent clogging.Similarly, the control valve 3 can be adjusted to provide for pulsatingoperation to prevent clogging of the valve by a control means 4.Preferably, this is done by opening the valve fully for a short time andthen turning it back to its normal position. This procedure isautomatically repeated with specified intervals.

Since it is normally not possible to avoid lump-forming totally, thoughit can be reduced to a minimum, as discussed above, it is preferred tocombine the present continuous discharge system with a conventionalbatchwise system, as shown in FIG. 1. In the present embodiment thebatch-wise discharge system is represented by a collecting tank 7, whichis connected to the gas phase reactor via a gas conduit. By batch-wisewithdrawal it is possible to prevent accumulation of lumps on thedistribution plate of the gas phase reactor 1. In a process according tothe present invention, the batchwise operated system can be designed fora substantially smaller capacity than conventionally and it can beoperated less frequently, for example only once an hour or even onlyonce a day. Generally one batchwise outlet nozzle should be enough forwithdrawal of lumps (polymer aggregates). The lumps can be detected byradioactive detection sensors.

Typically, if the reactor is provided with a discontinuous polymerdischarge system, the ratio between the polymer powder continuouslydischarged from the reactor to polymer powder discharge via thebatchwise operated system is about 1:1 to 10,000:1.

The degassing of the polymer powder takes place in at least onedegassing vessel, wherein the pressure of the gas flow is decreased toremove the gas from powder. The degassing section 18, 20 can comprise aproduct receiver 18 for separating gas from the polymer powder and a gassurge drum 20. The polymer powder is pneumatically conducted from thecollecting vessel 7 to the product receiver 18 or a second reactor.

The pressure of the gas from the gas collecting vessel can be increasedin a compressor 21 before the gas is recycled to a gas phase reactor,directly or through a recovery system/section.

FIG. 2 shows another preferred embodiment for continuous withdrawal. Theparts of the equipment are largely the same as in the previousembodiment, viz.:

-   31. gas phase reactor-   32. outlet nozzle of gas phase reactor-   33. control valve for gas-   34. level indicator/controller-   35. collecting tank-   36. recycle line-   37. screen-   38. outlet nozzle to remove lumps from collecting tank-   39. level indicator/controller-   40. control valve to regulate the flow of powder-   41. On-off valve for removal of lumps-   43, 45 collecting tanks of degassing section-   46 compressor

In the embodiment shown in FIG. 2, the outlet nozzle 32 of the gas phasereactor 31 is combined with a separate collecting vessel 35, which canbe used for separating lumps from the fluid comprising polymer powderand gas. The bed level of the gas phase reactor 31 is controlled by arecycle valve (control valve) 33 fitted in the recycle line 36 connectedto the gas space of the collecting vessel. Gas is recycled to the upperpart of the reactor above the fluidized bed and the bed height gives thenecessary pressure difference for conducting the polymer and the gas tothe collecting vessel 35.

The collecting vessel 35 is preferably provided with a separate levelcontroller 39 and a control valve 40 and polymer is pneumaticallyconducted under the influence of the pressure of the collecting vessel35 to a degassing vessel 43 or to a subsequent reactor. It is preferredto provide the collecting vessel with a screen 37 for collecting thelumps and with a separate discharge nozzle 38 for the lumps. The controlvalve 40 may be operated either intermittently or continuously. It ispreferred to operate the valve 40 continuously.

The operation of the degassing section 43-46 is similar to that of thefirst embodiment explained above.

The polymer continuously withdrawn can be directly or-indirectly fedinto another gas phase reactor.

The present invention can be used for producing homo- and copolymersfrom monomers selected from the group of C₂ to C₁₆ olefins and mixturesthereof. Preferably the monomer is ethylene, propylene, 1-butene,4-methyl-1-pentene, 1-hexene, a diene, or cyclic olefin, or a mixturesthereof.

The following non-limiting Examples illustrate the invention.

COMPARATIVE EXAMPLE

A production scale gas phase reactor was operated at 85° C. temperatureand 20 bar pressure with a bed level of 15 m as follows:

Polymer containing active polymerization catalyst was fed into the gasphase reactor from a loop reactor at a rate of 6 metric tons per hour.The feed rates of ethylene, hydrogen and 1-butene were adjusted so thatdesired concentrations in the gas phase reactor were reached. As aconsequence, the polymer production rate in the gas phase reactor was 8tons per hour and the polymer taken out of the reactor had an MFR₂₁, =11and density=947 kg/m³.

The polymer was collected from the reactor using a conventional,batchwise product outtake system, where the polymer was collected into a3.7 m³ receiving tank. Two identical systems were used. The diameter ofthe outtake nozzle was 8 inches. The period between two successiveouttakes was two minutes, i.e. four minutes for each individual system.During a normal operation the bed level was found to oscillate with a 20cm amplitude. The reactor could be operated several days without ashut-down.

An experiment to operate the product outtake with its maximum capacitywas made, and then the capacity was found to be 20 tons per hour.

EXAMPLE

A product outtake system according to the present invention wasinstalled in the gas phase reactor of the Comparative example. Thediameter of the nozzle was 2 inches (50 mm). Every minute the controlvalve was fully opened for a few seconds to prevent clogging of thevalve. The conventional discontinuous outtake was set to operate once anhour to remove any lumps from the reactor. No lumps were actuallycollected from the reactor during the test period and it was thusconcluded that the operation frequency of the discontinuous outlet couldhave been even lower.

The conditions of the reactor were similar to the Comparative example.During the normal operation the bed level was found to oscillate with a5 cm amplitude. The reactor was operated several days in a stablefashion until the test was interrupted.

In an experiment according to the Comparative example the maximumcapacity of the outtake was found to be 45 tons per hour.

1. A method of producing a polymer in a continuously operated gas phasereactor having two outlets from the reactor for collecting polymerproduct, the method comprising: polymerizing at least one monomer in abed containing active catalyst formed by catalyst and polymer particlessuspended in a fluid, said bed defining a fluidized bed level in saidreactor; continuously withdrawing polymer powder from the reactorthrough a first of the two outlets: adjusting a discharge rate of thepolymer powder so as to maintain a substantially constant bed levelduring polymerization; and separately recovering particle agglomeratesfrom the reactor by discontinuously withdrawing the particleagglomerates from a second of the two outlets, the second outlet beingdifferent from the first outlet, wherein the discharge rate of thepolymer powder is adjusted by using a continuously operated controlvalve, and the operation of the control valve is adjusted by using acontrol signal obtained from a bed level controller, and wherein thecontrol valve is adjusted to provide for pulsating operation to preventclogging of the valve.
 2. The method according to claim 1, wherein thecontinuously operated valve is a ball valve, a V-ball valve or a hosevalve.
 3. The method according to claim 2, wherein the first outletnozzle is connected to the control valve, and is provided with a gridflush mounted at the reactor wall to prevent lumps from entering thepipe.
 4. The method according to claim 1, wherein polymer powder iscontinuously withdrawn from a point above a fluidization plate.
 5. Themethod according to claim 1, wherein polymer powder is continuouslywithdrawn from a point below the bed level.
 6. The method according toclaim 1, wherein the discharge line and the control valve arediscontinuously backflushed with a flushing gas flow.
 7. The methodaccording to claim 1, further comprising using a gas phase reactorhaving a mechanically mixed zone of the fluidized bed, and continuouslywithdrawing the polymer powder from said mixed zone.
 8. The methodaccording to claim 1, wherein polymer powder is also separatelywithdrawn from the reactor using a discontinuous discharge device. 9.The method according to claim 1, wherein the polymer powder is withdrawntogether with gas from the reactor, the gas is separated from thepolymer powder, and the separated gas is recycled into the reactor. 10.A method of producing a polymer in a continuously operated gas phasereactor having two outlets from the reactor for collecting polymerproduct, comprising: polymerizing at least one monomer in a bedcontaining active catalyst formed by catalyst and polymer particlessuspended in a fluid, said bed defining a fluidized bed level in saidreactor; continuously withdrawing polymer powder from the reactorthrough a first of the two outlets; adjusting a discharge rate of thepolymer powder so as to maintain a substantially constant bed levelduring polymerization; and withdrawing particle agglomerates from thereactor with a discontinuously operated discharge valve from a second ofthe two outlets, the second outlet being different from the firstoutlet; wherein the discharge rate of the polymer powder is adjusted byusing a continuously operated control valve, and the operation of thecontrol valve is adjusted by using a control signal obtained from a bedlevel controller.
 11. A method of discharging polymer from acontinuously operated gas phase reactor having two outlets from thereactor for collecting polymer product, wherein at least one monomer ispolymerized in a bed containing active catalyst formed by catalyst andpolymer particles suspended in a fluid, said bed defining a fluidizedbed level in said reactor, comprising: continuously withdrawing polymerpowder from the reactor through a first of the two outlets; feeding thewithdrawn polymer powder into a collecting vessel, wherein lumps areseparated from finely-divided polymer powder and at least a part of thegas is separated from the solid material; recovering the lumps;separately recovering. additional particle agglomerates from the reactorby discontinuously withdrawing the particle agglomerates from a secondof the two outlets, the second outlet being different from the firstoutlet; and adjusting a discharge rate of the polymer powder so as tomaintain a substantially constant bed level during polymerization,wherein the discharge. rate of the polymer powder is adjusted by using acontinuously operated control valve, and the operation of the controlvalve is adjusted by using a control signal obtained from a bed levelcontroller.
 12. The method according to claim 11, wherein the separatedgas is recycled into the reactor, said collecting vessel being providedwith a return valve for adjusting the gas flow recycled to the reactor.13. The method according to claim 12, wherein the return valve iscontrolled by the fluidized bed level of the reactor.
 14. The methodaccording to claim 13, wherein the polymer level in the vessel iscontrolled by using a continuously operating control valve.
 15. Themethod according to any of claims 11 to 14, wherein the collectingvessel is provided with a screen for separating lumps.
 16. The methodaccording to claim 1, wherein the catalyst is fed into the gas phasereactor as a stream comprising polymer and active catalyst together withreaction medium.
 17. The method according to claim 16, wherein thecatalyst is fed into the gas phase reactor from a slurry reactor. 18.The method according to claim 17, wherein the slurry reactor is a loopreactor.
 19. The method according to claim 1, wherein the monomers areselected from the group of C₂ to C₁₆ olefins and mixtures thereof. 20.The method according to claim 1, wherein the monomer is selected fromthe group of ethylene, propylene, 1-butene, 4-methyl-1-pentene,1-hexene, dienes; and cyclic olefins, and mixtures thereof.
 21. Themethod according to claim 1, wherein the polymer that is continuouslywithdrawn is either directly or indirectly fed into another gas phasereactor.
 22. The method according to claim 11, wherein the collectingvessel is connected to a gas separator, said polymer powder beingpneumatically conducted from the collecting vessel to the gas separator.23. A method of producing a polymer in a continuously operated gas phasereactor having two outlets from the reactor for collecting polymerproduct, comprising: polymerizing at least one monomer in a bedcontaining active catalyst formed by catalyst and polymer particlessuspended in a fluid, said bed defining a fluidized bed level in saidreactor; continuously withdrawing polymer powder from the reactorthrough a first of the two outlets located at a point above afluidization plate where no lumps are present; adjusting a dischargerate of the polymer powder so as to maintain a substantially constantbed level during polymerization; and withdrawing particle agglomeratesfrom the reactor from a second of the two outlets, the second outletbeing different from the first outlet, located at the same level as thefluidized bed; wherein the discharge rate of the polymer powder isadjusted by using a continuously operated control valve, said operationof the control valve is adjusted by using a control signal obtained froma bed level controller.
 24. The method according to claim 1, wherein thestep of separately recovering the particle agglomerates from the reactoris accomplished by using an outlet located near a level of a distributorplate.
 25. The method according to claim 1, further comprising a step ofdegassing the polymer powder withdrawn from the reactor, wherein thepolymer powder is free-flowing powder.
 26. A method of producing apolymer in a continuously operated gas phase reactor having two outletsfrom the reactor for collecting polymer product, comprising:polymerizing at least one monomer in a bed containing active catalystformed by catalyst and polymer particles suspended in a fluid, said beddefining a fluidized bed level in said reactor; continuously withdrawingpolymer powder from the reactor through a first of the two outlets;adjusting a discharge rate of the polymer powder so as to maintain asubstantially constant bed level during polymerization; and separatelyrecovering particle agglomerates from the reactor by discontinuouslywithdrawing the particle agglomerates from a second of the two outlets,the second outlet being different from the first outlet, wherein thedischarge rate of the polymer powder is adjusted by using a continuouslyoperated control valve, and the operation of the control valve isadjusted by using a control signal obtained from a bed level controller,and wherein the first outlet nozzle is connected to the control valve,and is provided with a grid flush mounted at the reactor wall to preventlumps from entering the pipe.
 27. The process according to claim 1,wherein the first outlet nozzle and the second outlet nozzle aredirectly connected to a connecting tank which receives all theagglomerates and polymer from the fluidized bed reactor.
 28. The methodaccording to claim 1, wherein the ratio between the polymer powdercontinuously discharged from the reactor and the polymer particleagglomerates discontinuously withdrawn is in the range of 1:1 to10,000:1.
 29. The method according to claim 1, wherein a gas is returnedinto the gas phase reactor at a point above the level of the fluidizedbed.
 30. The method according to claim 1, wherein recovered lumps arewithdrawn from a collecting vessel through a second outlet nozzle.